WO2010022339A2 - Procédé et unité de capture de dioxyde de carbone - Google Patents

Procédé et unité de capture de dioxyde de carbone Download PDF

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Publication number
WO2010022339A2
WO2010022339A2 PCT/US2009/054626 US2009054626W WO2010022339A2 WO 2010022339 A2 WO2010022339 A2 WO 2010022339A2 US 2009054626 W US2009054626 W US 2009054626W WO 2010022339 A2 WO2010022339 A2 WO 2010022339A2
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WIPO (PCT)
Prior art keywords
carbon dioxide
packing
liquid
flow
rate
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Application number
PCT/US2009/054626
Other languages
English (en)
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WO2010022339A3 (fr
Inventor
David Keith
Maryam Mahmoudkhani
Alessandro Biglioli
Brandon Hart
Kenton Heidel
Mike Foniok
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1446881 Alberta Ltd.
Priority date (The priority date is an assumption and is not a legal conclusion. Google has not performed a legal analysis and makes no representation as to the accuracy of the date listed.)
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Publication date
Application filed by 1446881 Alberta Ltd. filed Critical 1446881 Alberta Ltd.
Priority to CA2734786A priority Critical patent/CA2734786C/fr
Priority to BRPI0917278-5A priority patent/BRPI0917278B1/pt
Priority to CN2009801379972A priority patent/CN102202766A/zh
Priority to MX2011001898A priority patent/MX2011001898A/es
Priority to EP09808878.4A priority patent/EP2321034B1/fr
Publication of WO2010022339A2 publication Critical patent/WO2010022339A2/fr
Publication of WO2010022339A3 publication Critical patent/WO2010022339A3/fr

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Classifications

    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/18—Absorbing units; Liquid distributors therefor
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/14—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols by absorption
    • B01D53/1456—Removing acid components
    • B01D53/1475—Removing carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01F—MIXING, e.g. DISSOLVING, EMULSIFYING OR DISPERSING
    • B01F23/00—Mixing according to the phases to be mixed, e.g. dispersing or emulsifying
    • B01F23/20—Mixing gases with liquids
    • B01F23/21—Mixing gases with liquids by introducing liquids into gaseous media
    • B01F23/214—Mixing gases with liquids by introducing liquids into gaseous media using a gas-liquid mixing column or tower
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B01D2251/304—Alkali metal compounds of sodium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/30—Alkali metal compounds
    • B01D2251/306—Alkali metal compounds of potassium
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2251/00—Reactants
    • B01D2251/60—Inorganic bases or salts
    • B01D2251/604—Hydroxides
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2257/00—Components to be removed
    • B01D2257/50—Carbon oxides
    • B01D2257/504—Carbon dioxide
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D2258/00—Sources of waste gases
    • B01D2258/06—Polluted air
    • B—PERFORMING OPERATIONS; TRANSPORTING
    • B01—PHYSICAL OR CHEMICAL PROCESSES OR APPARATUS IN GENERAL
    • B01D—SEPARATION
    • B01D53/00—Separation of gases or vapours; Recovering vapours of volatile solvents from gases; Chemical or biological purification of waste gases, e.g. engine exhaust gases, smoke, fumes, flue gases, aerosols
    • B01D53/34—Chemical or biological purification of waste gases
    • B01D53/74—General processes for purification of waste gases; Apparatus or devices specially adapted therefor
    • B01D53/77—Liquid phase processes
    • Y—GENERAL TAGGING OF NEW TECHNOLOGICAL DEVELOPMENTS; GENERAL TAGGING OF CROSS-SECTIONAL TECHNOLOGIES SPANNING OVER SEVERAL SECTIONS OF THE IPC; TECHNICAL SUBJECTS COVERED BY FORMER USPC CROSS-REFERENCE ART COLLECTIONS [XRACs] AND DIGESTS
    • Y02—TECHNOLOGIES OR APPLICATIONS FOR MITIGATION OR ADAPTATION AGAINST CLIMATE CHANGE
    • Y02C—CAPTURE, STORAGE, SEQUESTRATION OR DISPOSAL OF GREENHOUSE GASES [GHG]
    • Y02C20/00—Capture or disposal of greenhouse gases
    • Y02C20/40—Capture or disposal of greenhouse gases of CO2

Definitions

  • This document relates to gas-liquid contact systems and methods, including carbon dioxide capture systems and methods for the recovery of CO2 from atmospheric air.
  • Stolaroff et al. (2007) An alternative strategy, suggested by Stolaroff et al. (2007), is to generate a fine spray of the absorbing solution for providing large surface to the air flow through an open tower. This strategy could have the potential to operate with a small pressure drop in air and avoids the capital cost of packing material. Stolaroff et al. (2007) studied the feasibility of a NaOH spray- based contactor by estimating the cost and energy requirement per unit CO2 captured. Water loss, as a major concern in this design, was addressed and it was found that the water loss could be managed by adjusting of the NaOH concentration with temperature and humidity of air, i.e. the higher the concentration of sodium hydroxide, the lower is the water loss, e.g. using ⁇ 7.2M NaOH, at 15 0 C and 65% relative humidity, water loss is eliminated.
  • Conventional scrubbing towers may be filled with structured packing, and a flow of gas that is counter-current to the drainage of liquid through the structured packing is employed.
  • a carbon dioxide capture facility comprising packing formed as a slab, and at least one liquid source.
  • the slab has opposed dominant faces, the opposed dominant faces being at least partially wind penetrable to allow wind to flow through the packing.
  • the at least one liquid source is oriented to direct carbon dioxide absorbent liquid into the packing to flow through the slab.
  • the slab is disposed in a wind flow that has a nonzero incident angle with one of the opposed dominant faces.
  • a method of carbon dioxide capture is also disclosed.
  • Carbon dioxide absorbing liquid is applied into packing in a series of pulses.
  • a gas containing carbon dioxide is flowed through the packing to at least partially absorb the carbon dioxide from the gas into the carbon dioxide absorbing liquid.
  • the gas may flow continuously, even while the liquid flows intermittently.
  • the liquid and gas flow in a cross-flow geometry relative to one another.
  • cross-flow means that the direction of the flow of gas relative to the direction of the flow of liquid is orthogonal or perpendicular.
  • a method of carbon dioxide capture is also disclosed. Carbon dioxide absorbing liquid is flowed through packing in a mean liquid flow direction. A gas containing carbon dioxide is flowed through the packing obliquely or perpendicularly to the mean liquid flow direction to at least partially absorb the carbon dioxide from the gas into the carbon dioxide absorbing liquid.
  • a method of contacting a liquid with a gas is also disclosed.
  • the liquid is applied into packing in a series of pulses, and the gas is flowed through the packing.
  • a method of contacting a liquid with a gas is also disclosed.
  • the liquid is flowed through packing in a mean liquid flow direction.
  • the gas is flowed through the packing obliquely or perpendicularly to the mean liquid flow direction.
  • a gas-liquid contactor comprising packing, and at least one liquid source.
  • the packing is formed as a slab, the slab having opposed dominant faces, the opposed dominant faces being at least partially wind penetrable to allow wind to flow through the packing.
  • the at least one liquid source is oriented to direct the liquid into the packing to flow through the slab.
  • the slab is disposed in a wind flow that has a non-zero incident angle with one of the opposed dominant faces.
  • a gas-liquid contactor is also disclosed comprising a slab structure and a liquid source.
  • the slab structure comprises packing.
  • the liquid source is oriented to direct the liquid into the packing to flow in a mean liquid flow direction.
  • the slab structure is disposed in a wind flow that flows obliquely or perpendicularly to the mean liquid flow direction.
  • a method of contacting a liquid with a moving gas is also disclosed.
  • the liquid is flowed through packing, and the moving gas is driven through the packing in a drive direction that is at least partially oriented with an ambient flow direction of the moving gas.
  • Fig. 1 is a perspective view of a vertical slab contactor.
  • Fig. 2 is a side elevation view, in section, of a horizontal slab contactor.
  • Fig. 3 is a perspective view of the contactor of Fig. 2.
  • Fig. 4 is a top-down view of a series of carbon-dioxide capture facilities with a central processing facility.
  • Fig. 5 is a perspective view, including a series of exploded views thereof, of a horizontal slab contactor, partially in section.
  • Figs. 6 and 7 are graphs that illustrate the CCh removal from air passed through packing structured according to embodiments disclosed herein and pumped with liquid absorbent at different NaOH (Fig. 6) and KOH (Fig. 7) concentrations. Continuous flow is indicated by the dots on the y axis, while capture efficiency after a single pulse of flow is illustrated by the plotted lines.
  • Fig. 8 is a graph that illustrates the effectiveness of pulsed pumping of the liquid absorbent through the packing, by illustrating the CO2 removal per pulse at different NaOH concentrations.
  • Fig. 9 is a side elevation view of a vertical slab contactor with plural slabs.
  • the method involves directing ambient air using at least the energy of the wind, one or more fans, or both through a contactor comprising a packing material; intermittently flowing a carbon dioxide absorbing fluid over the packing to achieve an average flow rate; and, capturing CO 2 from the ambient air in the liquid such that either the carbon dioxide capture rate is increased relative to a similar method in which the liquid is constantly flowed at the average flow rate, or the effectiveness of cleaning the surface of the packing material is improved relative to a similar method in which the liquid is constantly flowed at the average flow rate, or both.
  • "Intermittantly flowing” means flowing a fluid at a first rate that is higher than at least one second rate (i.e. verying the flow of the fluid through the contactor) resulting in an average flow rate, wherein the at least one second rate can be zero. In some such embodiments, the at least one second rate is zero, and intermittently flowing produces a series of pulses.
  • the method involves intermittently flowing of a high molarity fluid through a contactor, and flowing ambient air through the contactor, thereby capturing CO2 from the ambient air. In some embodiments, the method involves intermittently flowing a high molarity fluid through a contactor in a cross- flow geometry relative to the direction of the flow of ambient air, thereby capturing CO 2 from the air. In some embodiments, the method involves intermittently flowing a high molarity fluid through a contactor in direction that is substantially perpendicular to the direction of flow of ambient air, thereby capturing CO 2 from the air. In some embodiments mentioned in this paragraph, "intermittently flowing" can be implemented as pulsing the fluid through the contactor (over the packing material).
  • the device is a carbon (or other ambient air component) capture facility including at least one liquid having a capacity to absorb carbon dioxide (or other ambient air component); at least one packing material having a hold up relative to the liquid; and, at least one pump for flowing the liquid over the packing material, the pump being configured to deliberately vary the flow rate to produce an average flow rate, wherein the capacity of the liquid and the holdup of the packing material are chosen to either cooperatively achieve an increased carbon dioxide capture rate relative to a similar carbon dioxide capture facility in which the pump is operated constantly at the average flow rate, or to improve the effectiveness of cleaning of the surface of the packing material relative to a similar carbon dioxide capture facility in which the pump is operated constantly at the average flow rate, or both.
  • the carbon capture facility comprises a packing material having sufficient hold up that it can be intermittently wetted with a CO 2 (or other ambient air component) capture solution, and the capture facility has a vertical slab geometry.
  • the capture facility comprises a packing material capable of being intermittently wetted and used in a cross-flow geometry, and the capture facility has a vertical slab geometry.
  • the capture facility comprises a packing material capable of being intermittently wetted and used in a substantially perpendicular geometry, and the capture facility has a vertical slab geometry.
  • the capture facility further comprises a device for removing dust contamination, for example structural stilts which can lift the capture facility off the ground, for example at least about 5m off of the ground so that dust blows underneath the facility.
  • the carbon capture facility can be built up in modules, such as for example illustrated in Fig. 1.
  • each module can have dimensions of about 5m by about 5m by bout 7m.
  • the modules contain packing and can support a fan. Once the modules are assembled to form the carbon capture facility, the packing material can ultimately occupy dimensions of about 200m by about 20m by about 3m.
  • the modules can be built from steel.
  • the final structure can include a sump at the base which has fluid.
  • a pump is configured to periodically moe the fluid from the supm to a distributor at the top of the packing.
  • the gas phase is moved through the packing by the wind, fans, or a combination thereof.
  • each module supports a fan, resulting in a wall of fans.
  • Packing is a material that fills a space and facilitates the contact between a gas stream and a liquid stream. Packing can be random or structured. Random packing comprises small shapes formed out of a suitable material and dumped into the space where contact between liquid and gas is to occur. Structured packing is any packing which is designed to be fitted into an area in a systematic and planned manner that results in a specific flow pattern for both air and liquid.
  • packing suitable for use within the scope of the disclosure has: a cross flow geometry designed to limit or minimize the pressure drop in air per unit CO2 extracted; can be efficiently wetted by intermittent liquid flows; and, has a liquid hold up enabling intermittent operation with long time durations between wetting.
  • packing suitable for use within the scope of the disclosure can tolerate manufacturing flaws, i.e. even significant portions of the packing material are not wetting.
  • packing suitable for use within the scope of the disclosure can include flaws or dead spots which are not wetted, as long as such dead spots do not significantly increase drag per unit CO 2 captured, or in other words the effect of the dead spots would not impact the overall cost per ton of CO 2 captured when both capital and operating costs are considered to an extent that would deter use of the packing material. In some embodiments, the effect of the dead spots would not increase the overall cost per ton Of CO 2 captured when both capital and operating costs are considered. In some embodiments, packing suitable for use within the scope of the disclosure includes up to about 10% dead spots or flaws. The use of packing with flaws or gas parts may reduce capital cost of the packing.
  • packing material suitable for use in accordance with the disclosure is readily cleaned of airborne contaminants. In some embodiments, cleaning should take advantage of intermittent flow. In some embodiments, packing suitable for use in carbon capture facilities within the scope of the disclosure are designed for liquid hold up, have a low resistance to the gas flow (e.g. about 100 Pa at gas flows of 2 m/s or less), and/or can be flushed by intermittent wetting.
  • the packing material can be chosen from low-density commercial structured packing.
  • low density commercial structured packing which is packing having a high void fraction, is thought to have a large area for the gas phase to pass through favorably impacting (i.e. reducing) the pressure drop across the packing relative packing with a lower void fraction.
  • a reduction in pressure drop is thought to lead to a decrease in the amount of energy consumed when moving the gas phase through the packing.
  • suitable packing materials include Bretwood AccuPak CF- 1200,
  • a “vertical slab” refers to a layout of packing in which the dimension parallel to gas flow is smaller than the dimensions perpendicular to the gas flow.
  • the thickness of the vertical slab (which is dimension parallel to the air flow) is about 3m, whereas the other two dimensions are about 200m (length) and 20m (height).
  • the liquid, or CO 2 capture solution which is used with the carbon capture facility, can be any liquid that can remove at least some CO 2 from ambient air.
  • a basic solution is used.
  • a KOH or a NaOH solution is used.
  • the KOH solution has a molarity ranging from less than 1 molar to about 6 molar.
  • the NaOH solution has a molarity ranging from less than 1 molar to about 6 molar.
  • the molarity of the solution can be chosen based on a number of factors, including location, packing structure, operating conditions, equipment and value of CO 2 captured. In general, the liquid is chosen to have a sufficient capacity to absorb CO 2 per unit volume to enable intermittent flow or wetting of the packing material.
  • the carbon capture facilities provide an improvement in one or more of operating costs, capital costs, and pressure drops (anywhere other than at the packing) relative to conventional ambient air carbon capture facilities comprising a packing material but having a cylindrical, tower geometry using a counterfiow design, specifically the tower geometry carbon capture facility described in
  • operating costs are improved by improving energy extraction from ambient wind to reduce energy use, for example by orienting the contactor to get the most energy from the wind, wherein the orientation is a function of wind directions and air handling equipment.
  • the slab is oriented so that the direction of the prevailing wind is not parallel to the direction of flow of the carbon capture solution through the packing material (i.e. the direction of the prevailing wind is not parallel to the orientation of the slab).
  • improved energy extraction from ambient air is accomplished using a cross-flow design.
  • the direction of the prevailing winds relative the orientation of the slab ranges from about 80 degrees to about 100 degrees. In general, the orientation would be chosen to minimize the annual average fan power depending on the wind rose and local geography.
  • the direction of the prevailing winds relative to the orientation of the slab is about 90 degrees.
  • operating costs are improved by intermittently wetting, rather than continuously dripping, the packing material with carbon capture liquid.
  • the carbon capture liquid is pulsed having a duration sufficient to wash the somewhat spent solution which is capturing CO2 at a reduced rate off the packing and replace it with fresh solution that will capture CO2 at a faster rate.
  • the time between pulses is chosen to reduce or minimize the cost of CO2 capture, taking into account both the energy required to operate the system and the cost of capital used to build the system.
  • the duration of a pulse can range from about 30 to about 60 seconds and the time between pulses can range from about 1 to about 20 minutes. In some embodiments, the duration of a pulse can range from about 60 to about 200 seconds and the time between pulses can range from about 1 to about 20 minutes. In some embodiments, the pump would be on for 150 seconds and off for 240 seconds In some embodiments, capital costs are reduced by reducing the footprint and total structure size per unit of capacity.
  • such packings may be operated using intermittent fluid flow.
  • High fluid flows i.e. fluid flows matching the specifications provided by the manufacturer
  • This operation mode can improve the overall energy efficiency by factors of three or more as compared to conventional counterflow tower geometries because the fluid pumping work is essentially eliminated.
  • "minimal loss of capture efficiency" can be demonstrated by an uptake rate decrease of less than 30% in a time span of minutes.
  • packing can be wetted using the flows suggested by the manufacturer's specifications but then the flow can be shut off and the uptake rate decreases by less than 30% in a time span of minutes.
  • FIGs. 6-8 there is provided laboratory data that demonstrates the first two ideas.
  • This data illustrates that commercial structured packing (e.g., Sultzer 250 X) can be operated with high molarity NaOH or KOH, for example, flowing in pulses that amount to less than, for example, 10% of full time (for example operating at the design fluid flow rate for about 30 seconds and then no fluid flow for about 600 seconds) while achieving >80% of the capture rate achieved with the design fluid flow rates.
  • the data would enable one to choose the optimal cycle time for specific contacting fluids and packing, and will provide a basis for improving packing designs for this application. Referring to Figs.
  • the total mechanical work requirement may be less than 100 kWhr/t-CO2 at capture rates greater than 20 t-CO2/m2-yr.
  • vertical slab geometry is emphasized in portions of this disclosure, disclosed as embodiments herein are two slab-geometry contactors: Vertical slab geometry (Fig. 1), and horizontal slab geometry (Figs. 2, 3, and 5). It should be understood that the disclosed embodiments are provided for the purpose of illustration and should not be construed as limiting in any way.
  • a carbon dioxide capture facility 10 comprising packing 12 formed as a slab 15, the slab 15 having opposed dominant faces 14, the opposed dominant faces 14 being at least partially wind penetrable to allow wind to flow through the packing 12.
  • At least one liquid source 16 is oriented to direct carbon dioxide absorbent liquid into the packing 12 to flow through the slab 15.
  • the slab 15 is disposed in a wind flow 18 that has a nonzero incident angle with one of the opposed dominant faces 14.
  • the packing 12 may be oriented to direct the flow of carbon dioxide absorbent liquid through the slab 15 in a mean flow direction 20 that is parallel to a plane 22 defined by the opposed dominant faces 14. It should be understood that opposed dominant faces 14 don't have to be exactly parallel.
  • the faces 14 may be converging, diverging, or curved for example.
  • Packing 12 may be oriented to allow the carbon dioxide liquid absorbent to flow through the packing 12 by gravity, as illustrated.
  • packing dimensions can be about 200m x about 20m by about 3m contained in a structure measuring about 200m x 25m x 7m. In some embodiments, dimensions can range from about 10m x about 7m x about 2m to about 1000m x about 50m x about 15m.
  • the non-zero incident angle refers to the fact that wind flow 18 strikes the face 14 at an angle greater than zero. This may be contrasted with traditional packing arrangements, where gas is flowed through a tower of packing starting from the very bottom.
  • the non-zero incident angle is orthogonal with the one of the opposed dominant faces. It should be understood that the non-zero incident angle may be within 10% of exactly orthogonal.
  • the non-zero incident angle may also refer to the mean angle of flow of the wind. The mean angle of flow of the wind may be averaged over a period of time.
  • the packing 12 further comprises structured packing.
  • the packing 12 may be, for example, 1-2 meters thick between the opposed dominant faces 14. In other embodiments, the packing 12 may be thicker or thinner.
  • the term structured packing may refer to a range of specially designed materials for use in absorption and distillation columns and chemical reactors. Structured packings typically consist of thin corrugated material 24, such as metal plates or gauzes arranged in a way that they force fluids to take complicated paths through the column, thereby creating a large face area for contact between different phases. Structured packings may be made out of corrugated sheets arranged in a crisscrossing relationship to create flow channels for the vapor phase. The intersections of the corrugated sheets create mixing points for the liquid and vapor phases. Wall wipers are utilized to prevent liquid and/or vapor bypassing along the column wall. Rotating each structured packing layer about the column axis provides cross mixing and spreading of the vapor and liquid streams in all directions.
  • the opposed dominant faces 14 may be oriented vertical.
  • the orientation of faces 14 may be determined relative to, for example, the ground. In other embodiments, faces 14 may be oriented at an angle to the ground, ie slanted.
  • the opposed dominant faces 14 may be oriented horizontal. This embodiment tends to have a larger footprint than the vertical slab embodiment.
  • the packing 12 is formed as plural slabs 15. Plural slabs may also be, for example, by plural slabs arranged end-to-end, as opposed to the stacked orientation illustrated in Fig. 9. In some embodiments, the slab might be vertically sectionalized, effectively providing plural slabs end to end on top of one another.
  • collector/distributor system that collects fluid flowing from above and redistributes it evenly to the packing slab below.
  • a collector/distributor system may be present in any slab as disclosed herein.
  • the at least one liquid source 16 may further comprise at least one pump 26.
  • Pump 26 may have several distribution pipes 28, controlled by a valve (not shown), in order to selectively apply liquid into various sections of packing 12.
  • the at least one pump 26 may be configured to supply the carbon dioxide absorbent liquid in a series of pulses.
  • At least one fan 30 may be oriented to influence wind flow through at least a section of one of the opposed dominant faces 14 of the packing 12. Fan 30 may be reversible. In some embodiments, fan 30 may prevent the wind flow that has already flowed through the packing 12 from circulating back into the packing 12. Referring to Fig. 5, in some embodiments, at least one fan 30 may drive the wind flow into packing 12. Referring to Fig. 1, the at least one fan 30 may further comprise plural fans, each of the plural fans being oriented to influence wind flow through at least a respective portion of the packing 12. In some embodiments, the respective portion is understood as being the portion of the packing 12 that air flow through fan 30 would have the greatest influence over, for example the packing 12 most adjacent or closest to fan 30.
  • the at least one fan 30 may provided as part of a fan wall 32 adjacent at least one of the opposed dominant faces 14. It should be understood that fan walls (not shown) may be located adjacent each of faces 14. Adjacent, in this document, is understood to mean next to, and can include embodiments (such as the one illustrated in the Figures) where the fan wall 32 is spaced from, but adjacent to, face 14. Referring to Fig. 1, the fan wall 32 may be adjacent the one of the opposed dominant faces 14 through which the wind flow 18 is exiting the packing 12. In fan wall 32, the individual fans may be separated by impermeable material. The fans 30 create a pressure drop across the wall 32, which drives flow through the packing 12.
  • fan wall 32 is designed such that, in the event that a fan fails, and ultimately blocks of its respective flow, flow through the packing 12 would be almost, if not completely, unaffected. This may be accomplished by closely spacing adjacent fans, and by spacing the fan wall 32 from the packing 12, for example.
  • facility 10 may further comprise wind guides 34 oriented to direct the flow of wind 18 into the packing 12.
  • Facility 10 may further comprise wind guides 36 oriented to direct the flow of wind 18 out of the packing 12.
  • Wind guides 34 and 36 may be, for example, louvers. As illustrated in Fig. 2, the wind guides 34 and 36 may be independently controllable. In the embodiment of Fig. 2, wind flow 18 is directed from the right to the left. Thus, the upper wind guides 34 are open, with the lower wind guides 34 closed. Similarly, upper wind guides 36 are closed, while lower wind guides 36 are open. Thus, wind flow 18 has a net flow from upper wind guides 24 to lower wind guides 36, passing through packing 12 in the process.
  • facility 10 may be part of an at least partially enclosed structure 38.
  • Wind guides 36 and 34 may aid in this, along with a surrounding structure adapted to selectively let in and process wind flow.
  • a protective covering (not shown) may be provided over packing 12 to prevent animal intrusion but allow wind flow to pass through.
  • a cleaning device 40 for cleaning the walls of the at least partially enclosed structure 38 may be provided. Cleaning device 40 may be, as illustrated for example, a wiper that rotates about an axis to clean the exterior of fan wall 32, for example.
  • Wind guides 34 and 36 may be horizontally oriented, for example. Referring to Fig.
  • facility 10 may further comprise at least one wind passage 42 extended through the opposed dominant faces 14 to deliver wind flow selectively to one of the opposed dominant faces 14.
  • wind passage 42 may have fan 30 attached to influence air flow through wind passage 42.
  • Wind passage 42 allows wind to travel through faces 14, where it is released into basin 44, where the wind is free to pass into packing 12 through face 14A, exiting the packing 12 through face 14B. This way, wind flow may be induced to flow through the horizontal faces 14 of a horizontal slab of packing 12.
  • Wind passages 42 may be, for example, air ducts that are 10 m in height.
  • wind passages 42 are vertical ducts in which CCh rich inlet air is moving down. These ducts may cover ⁇ l/5 of the surface area (e.g., ⁇ 1.2 m diameter tube arranged in a grid with 5 meter spacings.).
  • a sink 46 may be provided for collecting carbon dioxide absorbent liquid that has flowed through the packing 12.
  • the sink is illustrated as basin 44.
  • Basin 44 may be, for example a concrete-lined basin that catches the hydroxide and contains supports to hold the packing.
  • there may be a gap 60 as illustrated between the packing 12 and the base 44 that can be ⁇ 1 to 1.5 m for example.
  • sink 46 may be a pipe or a series of conduits for example, that transport the liquid directly from packing 12. This type of system may involve a funneling or drainage apparatus designed to focus the drainage of the liquid into a single, or a network of pipes.
  • facility 10 further comprises a recycling system 48 for regenerating spent carbon dioxide absorbent liquid.
  • the recycling system may be, for example, any of the systems disclosed in Appendix A, which forms part of this specification, for recycling spent carbon dioxide liquid absorbent.
  • the carbon dioxide absorbent liquid may comprise a hydroxide solution, for example a sodium hydroxide solution.
  • the source of liquid 16 preferably supplies recycled carbon dioxide absorbent liquid.
  • each pulse 50 may involve, for example, a short period during which the liquid is supplied into packing 12 by source of liquid 16.
  • Each pulse doesn't have to be a sharp transient application, but can be a period of time during which liquid is being supplied.
  • a gas containing carbon dioxide for example air illustrated by flow of wind 18, is flowed through the packing 12 to at least partially absorb the carbon dioxide from the gas into the carbon dioxide absorbing liquid.
  • Applying may further comprise pumping.
  • Flowing may further comprise flowing the gas containing carbon dioxide through the packing at least when the carbon dioxide absorbing liquid is not being applied. Referring to Fig.
  • the flow of gas may be controlled using fans 30, for example.
  • the flow of gas may be controlled using fans 30 and wind guides 34 and 36.
  • the flowing of the gas may be at least restricted when the carbon dioxide absorbing liquid is being applied. Referring to Fig. 1, this may be envisioned by the fans 30 of fan wall 32 ceasing to spin and draw the flow of wind through packing 12 when the pulse of liquid is being supplied to packing 12.
  • the series of pulses has a duty cycle of 1-50%. In other embodiments, such as the one illustrated graphically in Fig. 9, the duty cycle may be 5% for example.
  • the duty cycle refers to the ratio of the time duration of a pulse of applied liquid to the overall time duration of a cycle.
  • a 50% duty cycle implies the fluid is only flowing half the time the facility is operational. This means the pulse runs from 1 to 50% of the time the system is operational, and therefore a 1 % duty cycle means that for every second that fluid is flowing is off for 100 seconds. In more realistic values, it is on for 30 seconds and off for 3000 seconds and a 50% duty cycle means the pump would run for 30 seconds and be off for the next 30 seconds.
  • the series of pulses has an off-time of 10-1000 seconds. In other embodiments, the series of pulses has an off-time of 100-10000 seconds. Referring to Fig.
  • the step of applying may further comprise applying the carbon dioxide absorbing liquid into a first portion of the packing 12 in a first series of pulses, and applying the carbon dioxide absorbing liquid into a second portion of the packing 12 in a second series of pulses.
  • This may be envisioned by selectively applying liquid via distribution tubes 28A and 28B to packing 12. Because tubes 28A and 28B only feed a portion (ie the left-most portion) of packing 12, only that portion will have liquid applied to it. Liquid may then be selectively applied to the right hand portion of packing 12 by applying liquid via tubes 28C and 28D.
  • the first and second series of pulses may be synchronized, asynchronized, completely different, or synchronized out of phase with one another, for example, allowing fluids to be supplied intermittently from a continuously operating pump.
  • flowing the gas may further comprise at least restricting the flow of the gas containing carbon dioxide through the first portion of the packing when the carbon dioxide absorbing liquid is not being applied, and at least restricting the flow of the gas containing carbon dioxide through the second portion of the packing when the carbon dioxide absorbing liquid is not being applied.
  • the first portion has liquid being applied to it, for example the left hand portion of face 14 when liquid is being applied via tubes 28A and 28B, the flow of gas may be restricted or stopped altogether through the left hand portion of face 14.
  • the first series of pulses and the second series of pulses are staggered. Referring to Fig. 2, this may be advantageous, as when the left portion of face 14 has liquid being applied to it as described above, the right hand portion and center portions do not. Similarly, when the supply of liquid to the left hand portion is ceased, the source of liquid 16 may then apply liquid to the center or right hand portion, for example. This way, source of liquid 16 may cyclically feed liquid to the entire volume of packing 12 in a more efficient manner, instead of continuously feeding liquid to the entire volume of packing 12. Referring to Fig. 5, an example of this may be further envisioned, with a horizontal slab of packing 12.
  • the flow of wind through any of the various wind tubes 42 may be controlled, in order to achieve the same effect as that achieved above with the vertical slab embodiment.
  • Fig. 2 an embodiment is illustrated where only one wind tube 42A has wind being driven down it. This may be achieved by the selective actuation of fan 3OA, for example.
  • the packing 12 that is nearest the outlet of wind tube 42 A may have a flow of gas fed to it.
  • the off-cycle of the series of pulses may be less than or equal to the time it takes for carbon dioxide absorbing liquid to stop draining from the packing after a pulse. It should be understood that this is not the time required for the entire pulse to be removed from the packing 12, since some liquid will always be left over as residue inside the packing 12. In other embodiments, the off-cycle of the series of pulses may be less than or equal to the time it takes for a pulse of carbon dioxide absorbing liquid to lose 70-80 % of the pulses carbon dioxide absorption capacity.
  • the packing may be oriented to flow the carbon dioxide absorbing liquid through the packing 12 in a mean liquid flow direction 20.
  • Flowing may further comprise flowing the gas through the packing 12 obliquely or perpendicularly to the mean liquid flow direction 20.
  • this is advantageous as the flow of gas my have a different flow direction than, and one that is not counter current to, the mean liquid flow direction 20 of the liquid.
  • a larger surface area of the packing may be used to full advantage, greatly increasing the quantity of wind or gas that may contact liquid in packing 12 over a course of time while still allowing the liquid to pass through and drain from packing 12.
  • flowing the gas further comprises flowing the gas through the packing 12 perpendicularly to the mean liquid flow direction 20. It should be understood that exact perpendicularity is not a requirement.
  • Flowing may further comprise flowing the gas through at least one of the opposed dominant faces 14, for example through both of faces 14 as indicated. As disclosed above, these methods may involve recycling the carbon dioxide absorbing liquid. Also as disclosed above, the methods may involve influencing the flowing of the gas through the packing. Influencing may comprise, for example, preventing the gas that has already flowed through the packing 12 from circulating back into the packing 12.
  • Influencing may further comprise driving the flowing of the gas in a drive direction that is at least partially oriented with an ambient wind flow direction. This may be carried out using fans 30, which may be reversible in order to carry out this function. Further, these methods may involve directing the flow of gas at least one of into and out of the packing, using, for example louvers as already disclosed. Referring to Fig. 1, in some embodiments, fans 30 may be reversible in order to enable the flow to be driven in the direction of the ambient wind field, which is more efficient than inducing a flow that is counter to the prevailing wind direction. Referring to Fig.
  • the orientation of slabs 15 may be such that prevailing wind 18 is perpendicular to the slab 15, and is in the direction at which the fan wall (not shown) works most efficiently.
  • the packing design may use vertically oriented plates. This would be a modification of conventional structured packing designed to enable, for example, orthogonal liquid and gas flow directions. Packing may be for intermittent fluid flow so as to maximize the hold up of liquid absorbent inside the packing material.
  • the fan wall 32 may be sectionalized, so that flow speed can be reduced or stopped when fluid is flowing to minimize fluid loss. The sections may be operated asynchronously so that only one section at a time is receiving the fluid flow enabling fluid pumps to operate continuously.
  • the vertical slab minimizes the footprint and the total structure size per unit of capacity to reduce the capital cost, reduces peak velocity, improving efficiency, and enables the packing to be operated at higher peak velocities further reducing capital costs.
  • some embodiments may invoke the use of louvers to enable the flow to be driven in the direction of the ambient wind without altering the operation of the fans.
  • the packing design may using coaxial flow or counter current flow, while still benefiting from the larger surface area of the slab to increase the amount of wind flow through the slab.
  • the flow geometry allows one to get even flow though a large horizontal slab mounted just above a fluid reservoir while maintaining air speeds below about 5 m/sec.
  • the air speed constraint determines the ratio of the structures height to its width. Specifically, height/width is approximately equal to airspeed-at-packing/air-speed-at-exit.
  • the horizontal slab has a larger footprint, and may have higher costs, but it has the advantage that it may use more conventional packing and fluid distribution.
  • a rough sketch is illustrated showing a mile X mile grid (eg. roads on a North American prairie) with 8 capture units each having, for example, 300 X 50 m footprint facilities 10 and a central processing station 48 with connecting pipelines 56.
  • a system of this magnitude would be expected to capture 1-5 megatons CO2 per year.
  • a view of a full unit for example 50 m wide, by 300 long, by 20 m high is illustrated.
  • the height of the slabs may be 10 - 30 m. If the wind was blowing from the right to left, one would open the louvers so that inlet air flowed in on the lower right and out the upper left. (This is the opposite of what is shown in the cross section illustrated in Fig. 2).
  • the roof 58 may be rough, like the zig-zag design shown here which is structurally efficient. In some embodiments, the roof 58 need not keep water out, it need only be proof against wind loads.
  • the source of liquid may be, for example a fluid distribution system on top of packing 12.
  • Carbon dioxide absorbing liquid is flowed through packing 12 in a mean liquid flow direction 20
  • a gas containing carbon dioxide is flowed through the packing 12 obliquely or perpendicularly to the mean liquid flow direction 20 to at least partially absorb the carbon dioxide from the gas into the carbon dioxide absorbing liquid.
  • Flowing carbon dioxide absorbing liquid through packing 12 may further comprise applying the carbon dioxide absorbing liquid into the packing 12 in a series of pulses. The series of pulses has been disclosed in detail throughout this document, and need not be built upon here.
  • flowing the gas further may comprise flowing the gas through the packing 12 perpendicularly to the mean liquid flow direction 20.
  • a method of contacting a liquid with a gas comprising applying the liquid into packing 12 in a series of pulses and flowing the gas through the packing 12.
  • the downward slope of each of the profiles indicates that CO 2 is still being absorbed by the slowly draining or stagnant liquid. This illustrates that this packing 12 design is highly efficient, because it continues to effectively contact gas and liquid, without the need for constant pumping.
  • the capture efficiency of CO 2 is illustrated and contrasted for continuous flow (indicated by the dots on the y axis), and for a single pulse of flow (illustrated by the plotted lines).
  • the time scale is time after the flow has been shut off for the pulsed flow.
  • the downward sloping lines show the gradual drop off in capture efficiency over 200- 1000 seconds, but illustrate that the liquid still has a high capture efficiency, even after hundreds of seconds have passed. While this method is also envisioned for some of the embodiments herein, it is not as efficient as the pulsed method, as it requires far greater pumping action. Thus, the pulsed method may be applied to any gas-liquid contactor, because it has been proven herein to afford sufficient gas-liquid contact despite a lack of continuous pumping. An exemplary application of this may be provided as a scrubbing unit at a refinery, for example. It should be understood that the gas-liquid contactor may have all of the same characteristics as the carbon dioxide capture facility as disclosed herein.
  • a method of contacting a liquid with a gas comprising flowing the liquid through packing in a mean liquid flow direction, and flowing the gas through the packing obliquely or perpendicularly to the mean liquid flow direction.
  • This method may be envisioned as carried out by the embodiments in the figures. Similar to the gas-liquid contactor, the results from Figs. 6-8 confirm that this method may be applied to any gas-liquid contact system.
  • the structure of such a contactor employing this method would be greatly simplified, since the gas inlet and outlet will be at different locations in the packing then the liquid source and sink. This is in contrast to previous systems which supply gas in a counter-current direction to the liquid flow.
  • flowing the liquid through the packing may further comprise applying the liquid into the packing in a series of pulses.
  • flowing the gas may further comprise flowing the gas through the packing perpendicularly to the mean liquid flow direction.
  • a gas-liquid contactor (illustrated by facility 10) is also disclosed.
  • the contactor (illustrated as facility 10) comprises packing 12 formed as a slab 15, the slab 15 having opposed dominant faces 14, the opposed dominant faces 14 being at least partially wind penetrable to allow wind to flow through the packing 12.
  • At least one liquid source 16 is oriented to direct the liquid into the packing 12 to flow through the slab 15.
  • the slab is disposed in a wind flow 18 that has a non-zero incident angle with one of the opposed dominant faces 14.
  • the results from Figs. 6-8 confirm that this method may be applied to any gas-liquid contactor. It should be understood that this gas-liquid contactor may have all of the same characteristics as the carbon dioxide capture facility and contactor disclosed herein.
  • a gas-liquid contactor (illustrated by facility 10) is also disclosed, comprising a slab 15 structure comprising packing 12 and a liquid source 16 oriented to direct the liquid into the packing 12 to flow in a mean liquid flow direction 20.
  • the slab structure is disposed in a wind flow 18 that flows obliquely or perpendicularly to the mean liquid flow direction 20.
  • the results from Figs. 6-8 confirm that this method may be applied to any gas-liquid contactor. It should be understood that this gas-liquid contactor may have all of the same characteristics as the carbon dioxide capture facility and contactor disclosed herein.
  • a method of contacting a liquid with a moving gas (illustrated as wind flow 18) is disclosed.
  • the method comprises flowing the liquid through packing 12, and driving the moving gas through the packing 12 in a drive direction (illustrated as 18B, which is the same as wind direction 18 in this embodiment) that is at least partially oriented with an ambient flow direction 18 of the moving gas.
  • the flowing gas is wind
  • the ambient flow direction is the ambient wind direction 18.
  • This method may further comprise reversing the drive direction 18B when the ambient flow direction 18 reverses.
  • Reversing the fan direction (or more generally, reversing the forced flow of air through the packing) in such a way as to drive the air with a vector direction that is at least partially oriented with the ambient wind 18 reduces the required fan power. Further, this reduces the amount of Io W-CO 2 air that is recycled back into the inlet of the system, thus improving its efficiency. It is thus advantageous to align the packing such that one of opposed dominant face 14 is roughly perpendicular to the prevailing wind, in order to maximize the efficiency of the fans.
  • wind flow is understood as moving gas containing CO 2 .
  • the carbon that is sequestered from a gas comprising carbon dioxide using the methods described herein can be equated with, for example, an environmental credit such as a carbon credit.
  • Carbon credits are used to provide an incentive to reduce greenhouse gas emissions by capping total annual emissions and letting the market assign a monetary value to a tradable unit.
  • carbon credits include carbon credits as defined by provisions in place at the time of filing but are not limited to such.
  • Carbon credits also refer to any type of tangible or intangible currency, stocks, bonds, notes or other tradable or marketable unit used to value an amount of carbon sequestered, an amount of greenhouse gas emissions reduced, or any other type of carbon-neutral or carbon-negative activities.
  • a similar concept of environmental credits can be applied, for example, for the implementation of best practices related to environmental land practices.
  • Carbon credits can be obtained, for example, by applying and receiving certification for the amount of carbon emissions reduced (e.g., the amount of carbon sequestered, the amount of CO2 and other greenhouse gases not released into the atmosphere).
  • the quality of the credits can be based in part on validation processes and the sophistication of funds or development companies that act as sponsors to carbon projects. See, for example, U.S. Patent Publication Nos. 2002/0173979 and 2007/0073604 for representative methods for verifying and valuing carbon credits.
  • Carbon credits can be exchanged between businesses or bought and sold in national or international markets at a prevailing market price.
  • companies can sell carbon credits to commercial and individual customers who are interested in voluntarily offsetting their carbon footprints. These companies may, for example, purchase the credits from an investment fund or a carbon development company that has aggregated the credits from individual proj ects .
  • the process of applying for, obtaining and/or validating one or more carbon credits may or may not include taking actual measurements.
  • each transfer of carbon credits within Europe is validated by the ETS, and each international transfer is validated by the United Nations Framework Convention on Climate Change (UNFCCC).
  • UNFCCC United Nations Framework Convention on Climate Change
  • the word "comprising” is used in its inclusive sense and does not exclude other elements being present.
  • the indefinite article "a" before a claim feature does not exclude more than one of the feature being present.
  • Each one of the individual features described here may be used in one or more embodiments and is not, by virtue only of being described here, to be construed as essential to all embodiments as defined by the claims.

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Abstract

L'invention concerne une unité de capture de dioxyde de carbone comprenant un garnissage réalisé sous la forme d'une plaque, et au moins une source de liquide. La plaque se compose de faces dominantes opposées que le vent peut pénétrer au moins en partie afin de traverser le garnissage. La ou les sources de liquide sont orientées de manière à guider le liquide absorbant le dioxyde de carbone dans le garnissage et permettre au liquide de s’écouler dans la plaque. La plaque est installée sous un flux de vent qui présente un angle incident non nul avec l'une des faces dominantes opposées. L’invention a trait en outre à un procédé de capture du dioxyde de carbone. Le liquide absorbant le dioxyde de carbone est introduit dans le garnissage suivant une série d'impulsions. Un gaz renfermant du dioxyde de carbone s’écoule dans le garnissage afin de permettre au liquide absorbant le dioxyde de carbone d’absorber au moins partiellement le dioxyde de carbone présent dans le gaz.
PCT/US2009/054626 2008-08-21 2009-08-21 Procédé et unité de capture de dioxyde de carbone WO2010022339A2 (fr)

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Application Number Priority Date Filing Date Title
CA2734786A CA2734786C (fr) 2008-08-21 2009-08-21 Procede et unite de capture de dioxyde de carbone
BRPI0917278-5A BRPI0917278B1 (pt) 2008-08-21 2009-08-21 Instalação de captura de dióxido de carbono
CN2009801379972A CN102202766A (zh) 2008-08-21 2009-08-21 二氧化碳捕获方法和设施
MX2011001898A MX2011001898A (es) 2008-08-21 2009-08-21 Metodo de captura de dioxido de carbono e instalacion.
EP09808878.4A EP2321034B1 (fr) 2008-08-21 2009-08-21 Procédé et unité de capture de dioxyde de carbone

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US9086708P 2008-08-21 2008-08-21
US61/090,867 2008-08-21

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WO2010022339A2 true WO2010022339A2 (fr) 2010-02-25
WO2010022339A3 WO2010022339A3 (fr) 2010-05-27

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EP (1) EP2321034B1 (fr)
CN (2) CN106621705A (fr)
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CA (1) CA2734786C (fr)
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WO (1) WO2010022339A2 (fr)

Cited By (21)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
WO2014170184A1 (fr) 2013-04-18 2014-10-23 Climeworks Ag Structure a faible chute de pression de lit adsorbant de particules pour un procede de separation de gaz par adsorption
WO2014164738A3 (fr) * 2013-03-13 2014-12-24 Carbon Engineering Limited Partnership Recueil d'une solution caustique au moyen d'agrégats de cristaux de carbonate de calcium
WO2016005226A1 (fr) 2014-07-10 2016-01-14 Climeworks Ag Procédé de désorption sous vide assistée par de la vapeur pour capturer du dioxyde de carbone
US9637393B2 (en) 2014-05-19 2017-05-02 Carbon Engineering Limited Partnership Recovering a caustic solution via calcium carbonate crystal aggregates
WO2018083109A1 (fr) 2016-11-04 2018-05-11 Climeworks Ag Structure à faible chute de pression d'un lit d'adsorption de particules pour un procédé amélioré de séparation de gaz par adsorption
WO2018210617A1 (fr) 2017-05-15 2018-11-22 Climeworks Ag Structure à faible chute de pression de lit adsorbant de particules pour procédé de séparation de gaz par adsorption
US10232305B2 (en) 2014-06-03 2019-03-19 Climeworks Ag Direct air capture device
US10421039B2 (en) 2016-06-14 2019-09-24 Carbon Engineering Ltd. Capturing carbon dioxide
US10427086B2 (en) 2013-04-18 2019-10-01 Climeworks Ag Low-pressure drop structure of particle adsorbent bed for adsorption gas separation process
WO2019238488A1 (fr) 2018-06-14 2019-12-19 Climeworks Ag Procédé et dispositif d'adsorption/désorption de dioxyde de carbone à partir de flux gazeux avec unité de récupération de chaleur
EP3673972A1 (fr) 2018-12-28 2020-07-01 Vito NV Capture et utilisation de dioxyde de carbone à médiation alcaline
WO2020154518A1 (fr) 2019-01-23 2020-07-30 Blue Planet, Ltd. Compositions d'agrégats de carbonate et leurs procédés de préparation et d'utilisation
WO2020254208A1 (fr) 2019-06-21 2020-12-24 Climeworks Ag Structure d'adsorbant pour processus de séparation de gaz
US11007470B2 (en) 2013-04-18 2021-05-18 Climeworks Ag Low-pressure drop structure of particle adsorbent bed for improved adsorption gas separation process
WO2021099695A1 (fr) 2019-11-19 2021-05-27 Arkolia Energies Installation de production de méthane
WO2021239747A1 (fr) 2020-05-29 2021-12-02 Climeworks Ag Procédé de capture de dioxyde de carbone à partir d'air ambiant et structures adsorbantes correspondantes avec une pluralité de surfaces parallèles
US11504667B2 (en) 2008-08-21 2022-11-22 Carbon Engineering Ltd. Carbon dioxide capture method and facility
WO2024006506A1 (fr) 2022-07-01 2024-01-04 W. L. Gore & Associates, Inc. Structure avec support externe pour lit adsorbant de particules pour processus de séparation de gaz d'adsorption
WO2024039641A1 (fr) 2022-08-15 2024-02-22 W. L. Gore & Associates, Inc. Structures et procédés pour améliorer la capture de dioxyde de carbone de l'air ambiant
US12006580B2 (en) 2018-04-25 2024-06-11 The University Of British Columbia Systems and methods for electrochemical generation of syngas and other useful chemicals
WO2024129714A2 (fr) 2022-12-13 2024-06-20 W. L. Gore & Associates, Inc. Structure à faible chute de pression d'un lit d'adsorption de particules pour un procédé amélioré de séparation de gaz par adsorption

Families Citing this family (35)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US8119091B2 (en) * 2008-06-20 2012-02-21 Carbon Engineering Limited Partnership Carbon dioxide capture
WO2012109379A2 (fr) * 2011-02-08 2012-08-16 Phycal Inc. Système de gestion du carbone
AU2012296378B2 (en) 2011-08-17 2016-06-02 1234 10Th Street Llc Reducing the carbon emissions intensity of a fuel
WO2013036859A1 (fr) 2011-09-07 2013-03-14 Carbon Engineering Limited Partnership Capture de gaz cible
WO2013098201A1 (fr) * 2011-12-28 2013-07-04 Antecy B.V. Procédé de production d'un combustible liquide à partir d'un courant gazeux comprenant du dioxyde de carbone
WO2015042315A1 (fr) 2013-09-18 2015-03-26 James Rhodes Réduction de l'intensité des émissions de carbone d'un combustible
WO2016160612A1 (fr) * 2015-03-27 2016-10-06 Blue Planet, Ltd. Unités et systèmes de séquestration de co2 modulaires, et procédés d'utilisation de ceux-ci
EP3199215B8 (fr) * 2016-01-27 2019-01-02 Loratech Ag Appareil et procécé pour la mise en contact d'un gaz et d'un liquide
AU2017383560B2 (en) * 2016-12-23 2023-05-25 Carbon Engineering Ltd. Method and system for synthesizing fuel from dilute carbon dioxide source
US11844541B2 (en) * 2017-02-03 2023-12-19 Aggreko, Llc Cooling tower
WO2020014188A1 (fr) 2018-07-09 2020-01-16 The Regents Of The University Of Michigan Système de surveillance de microscope
AU2019369241A1 (en) 2018-10-29 2021-05-20 Arizona Board Of Regents On Behalf Of Arizona State University Device, system, and method for passive collection of atmospheric carbon dioxide
WO2020154545A1 (fr) * 2019-01-23 2020-07-30 Evapco, Inc. Tour de capture de dioxyde de carbone
EP3725391B1 (fr) * 2019-04-18 2021-05-26 Climeworks AG Dispositif de capture de co2 de l'air à haut rendement et son procédé de fonctionnement
US20220348461A1 (en) 2019-09-27 2022-11-03 Oxy Low Carbon Ventures, Llc Process for the conversion of carbon dioxide
KR20230004843A (ko) 2020-05-04 2023-01-06 인피니움 테크놀로지, 엘엘씨 역수성 가스 전이 촉매 반응기 시스템
US11560343B2 (en) 2020-05-04 2023-01-24 Infinium Technology, Llc Process for capture of carbon dioxide from air and the direct conversion of carbon dioxide into fuels and chemicals
CA3204926A1 (fr) 2020-05-04 2021-11-11 Infinium Technology, Llc Procede de conversion de dioxyde de carbone et d'energie en combustibles et en produits chimiques
US11498886B2 (en) 2020-05-04 2022-11-15 Infinium Technology, Llc Catalysts and processes for the direct production of liquid fuels from carbon dioxide and hydrogen
AU2021385488A1 (en) * 2020-11-30 2023-06-22 Arizona Board Of Regents On Behalf Of Arizona State University Device and method for passive carbon dioxide collection with suspended sorbent disks
CA3200293A1 (fr) * 2020-12-21 2022-06-30 David St. Angelo Capture de dioxyde de carbone
US12104125B2 (en) 2021-02-05 2024-10-01 Infinium Technology, Llc Efficient 2-step process for the direct production of liquid fuels from carbon dioxide and hydrogen
GB202106841D0 (en) 2021-05-13 2021-06-30 Air View Enhineering Ltd Gas separation apparatus
US11389761B1 (en) 2021-06-11 2022-07-19 Joseph J. Stark System and method for improving the performance and lowering the cost of atmospheric carbon dioxide removal by direct air capture
US11266951B1 (en) 2021-06-11 2022-03-08 Joseph J. Stark System and method for improving the performance and lowering the cost of atmospheric carbon dioxide removal by direct air capture
US11266943B1 (en) * 2021-06-11 2022-03-08 Joseph J. Stark System and method for improving the performance and lowering the cost of atmospheric carbon dioxide removal by direct air capture
US11305230B1 (en) * 2021-11-13 2022-04-19 Marvin S Keshner Direct capture of carbon dioxide from air
US12036507B2 (en) 2022-02-15 2024-07-16 International Business Machines Corporation Compressible fluid separator pump
WO2023161404A1 (fr) 2022-02-25 2023-08-31 Fld Technologies Gmbh Méthode d'élimination et d'immobilisation de dioxyde de carbone de l'atmosphère et/ou d'un gaz résiduaire
US11813565B1 (en) 2022-04-29 2023-11-14 Klöckner Pentaplast Of America, Inc. Materials having improved wettability and related methods of use and manufacture
EP4309767A1 (fr) 2022-07-19 2024-01-24 Consejo Superior De Investigaciones Científicas (CSIC) Procédé de capture de co2 à partir de l'atmosphère et dispositif de contacteur d'air conçu pour exécuter le procédé de capture de co2
CN115178059B (zh) * 2022-08-17 2023-12-22 胡怡文 一种建筑环境碳中和排放处理设备
GB2624380A (en) * 2022-11-10 2024-05-22 Rolls Royce Plc Direct air capture system with eddy generation
GB2624211A (en) * 2022-11-10 2024-05-15 Rolls Royce Plc Direct air capture system and method
US12017179B1 (en) 2023-08-15 2024-06-25 AirMyne, Inc. Interfacial surface structures for carbon dioxide removal systems

Family Cites Families (66)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US3363885A (en) * 1964-12-22 1968-01-16 Munters & Co Modular cooling tower
SE325589B (fr) * 1967-02-21 1970-07-06 C G Munters
JPS5112724B2 (fr) 1974-02-23 1976-04-22
US4049399A (en) * 1975-04-08 1977-09-20 Teller Environmental Systems, Inc. Treatment of flue gases
US4183901A (en) 1976-01-23 1980-01-15 Fmc Corporation Process for crystallization of anhydrous sodium carbonate
US4031180A (en) * 1976-06-22 1977-06-21 Acme Eng. & Mfg. Corporation Cooling pad system
US4200264A (en) 1976-08-16 1980-04-29 Fumio Hori Apparatus for obtaining Mg and Ca through carbon reduction
US4215079A (en) * 1978-03-22 1980-07-29 Donaldson Company, Inc. Method and apparatus for contacting liquids and gases
US4401635A (en) 1979-11-13 1983-08-30 Intermountain Research And Development Corporation Recovery of alkali values from salt-containing trona deposits
US4251494A (en) 1979-12-21 1981-02-17 Exxon Research & Engineering Co. Process for removing acidic compounds from gaseous mixtures using a two liquid phase scrubbing solution
US4344650A (en) 1980-01-21 1982-08-17 Fmc Corporation Recovery of alkali values from trona deposits
US4632760A (en) 1980-08-18 1986-12-30 Donald N. Hanson Method of treating aqueous solutions
US4676934A (en) * 1985-09-27 1987-06-30 Jaeger Products, Inc. Structured WV packing elements
US5364604A (en) * 1987-03-02 1994-11-15 Turbotak Technologies Inc. Solute gas-absorbing procedure
DE4104447A1 (de) * 1991-02-14 1992-08-20 Sigri Gmbh Korrosions- und hitzebestaendige geordnete packung fuer stoff- und waermeaustauschprozesse
US5227095A (en) * 1991-11-27 1993-07-13 Curtis Harold D Modular cooling tower
US5283054A (en) 1993-03-30 1994-02-01 Fmc Corporation Process for producing sodium salts from brines of sodium ores
US5582683A (en) 1994-04-19 1996-12-10 International Paper Company Method for the recovery of chemical values from black liquor in multiple streams of different chemical values
US5695548A (en) * 1995-11-13 1997-12-09 Trutna; William R. Method and apparatus for producing co-current fluid contact
US5679131A (en) 1996-03-13 1997-10-21 Photran Corporation Method for producing titanium oxide from ore concentrates
DE19629500C1 (de) * 1996-07-22 1998-04-16 Thermoselect Ag Multiwäscher und Verfahren zur Totalreinigung von Gasen
US6068686A (en) * 1997-10-07 2000-05-30 Sorensen; Ian W. Scrubber system and method of removing pollutants from a fluid
SE9802463D0 (sv) 1997-12-22 1998-07-08 Munters Ab Air treatment unit
GB9925992D0 (en) * 1999-11-04 2000-01-12 Aerotech Engineering Ltd Filter
US6428759B1 (en) 2000-05-02 2002-08-06 Fmc Wyoming Corporation Production of feed liquors for sodium carbonate crystallization processes
US6372022B1 (en) * 2000-08-10 2002-04-16 Air Liquide America Corporation Ionic purifier
US6843835B2 (en) * 2001-03-27 2005-01-18 The Procter & Gamble Company Air cleaning apparatus and method for cleaning air
US6582498B1 (en) * 2001-05-04 2003-06-24 Battelle Memorial Institute Method of separating carbon dioxide from a gas mixture using a fluid dynamic instability
US20030097936A1 (en) * 2001-11-27 2003-05-29 Robert Maleeny Air scenting compositions and processes for use thereof in air scenting devices
US6875250B2 (en) * 2002-05-06 2005-04-05 Honeywell International Inc. Deep filter element suitable for replacing a shallow filter element and having a support frame made from thin stock
US7214290B2 (en) 2002-09-04 2007-05-08 Shaw Liquid Solutions Llc. Treatment of spent caustic refinery effluents
US6840987B1 (en) * 2003-01-10 2005-01-11 Eliu P. Gonzalez Air filtering apparatus
SG115648A1 (en) * 2003-03-31 2005-10-28 Air Prod & Chem Structured packing with increased capacity
US7005076B2 (en) * 2003-06-06 2006-02-28 Rmt, Inc. Caustic solution treatment process
US7699909B2 (en) * 2004-05-04 2010-04-20 The Trustees Of Columbia University In The City Of New York Systems and methods for extraction of carbon dioxide from air
US7947239B2 (en) * 2004-05-04 2011-05-24 The Trustees Of Columbia University In The City Of New York Carbon dioxide capture and mitigation of carbon dioxide emissions
WO2006009600A2 (fr) 2004-05-04 2006-01-26 The Trustees Of Columbia University In The City Of New York Systemes et procedes pour l'extraction de dioxyde de carbone dans de l'air
US20060000196A1 (en) * 2004-07-02 2006-01-05 Beier Scott B Fluid filter
US20060051274A1 (en) * 2004-08-23 2006-03-09 Wright Allen B Removal of carbon dioxide from air
US7727374B2 (en) 2004-09-23 2010-06-01 Skyonic Corporation Removing carbon dioxide from waste streams through co-generation of carbonate and/or bicarbonate minerals
US7314847B1 (en) 2004-10-21 2008-01-01 The United States Of America As Represented By The United States Department Of Energy Regenerable sorbents for CO2 capture from moderate and high temperature gas streams
WO2006050196A2 (fr) * 2004-10-29 2006-05-11 Eisenmann Corporation Systeme d'injection de gaz naturel d'un oxydeur thermique regeneratif
RU2424041C2 (ru) * 2005-02-02 2011-07-20 ГЛОБАЛ РИСЕРЧ ТЕКНОЛОДЖИЗ, ЭлЭлСи Удаление диоксида углерода из воздуха
US7297182B2 (en) * 2005-03-02 2007-11-20 Eisenmann Corporation Wet electrostatic precipitator for treating oxidized biomass effluent
US7318857B2 (en) * 2005-03-02 2008-01-15 Eisenmann Corporation Dual flow wet electrostatic precipitator
US20070148069A1 (en) 2005-12-23 2007-06-28 Shrikar Chakravarti Carbon dioxide recovery from flue gas and the like
US7740691B2 (en) * 2006-01-10 2010-06-22 Edwin W. Cash Gas treating method and apparatus
US20080011161A1 (en) * 2006-07-17 2008-01-17 General Electric Company Carbon dioxide capture systems and methods
KR20090086530A (ko) 2006-10-02 2009-08-13 글로벌 리서치 테크놀로지스, 엘엘씨 공기로부터 이산화탄소를 추출하는 방법 및 장치
US7708803B2 (en) * 2006-11-03 2010-05-04 Electric Power Research Institute, Inc. Method and apparatus for the enhanced removal of aerosols from a gas stream
CN100493673C (zh) * 2007-05-15 2009-06-03 大连理工大学 回收混合气体中二氧化碳的复合脱碳溶液
US7645430B2 (en) * 2007-10-08 2010-01-12 Alcoa Inc. Systems and methods for removing gaseous pollutants from a gas stream
US8414853B2 (en) * 2008-03-21 2013-04-09 Alstom Technology Ltd System and method for enhanced removal of CO2 from a mixed gas stream via use of a catalyst
US8119091B2 (en) 2008-06-20 2012-02-21 Carbon Engineering Limited Partnership Carbon dioxide capture
US9095813B2 (en) 2008-08-21 2015-08-04 Carbon Engineering Limited Partnership Carbon dioxide capture method and facility
AU2012296378B2 (en) * 2011-08-17 2016-06-02 1234 10Th Street Llc Reducing the carbon emissions intensity of a fuel
EP2782657B1 (fr) 2011-11-25 2016-12-28 Climeworks AG Système d'extraction de dioxyde de carbone réparti intégré dans un bâtiment, conçu pour réduire les besoins en air neuf
US20150139887A1 (en) 2012-07-17 2015-05-21 Antecy B.V. Materials and process for reversible adsorption of carbon dioxide
NO2986357T3 (fr) 2013-04-18 2018-07-14
US10350547B2 (en) 2013-12-03 2019-07-16 Antecy B.V. Moisture swing carbon dioxide enrichment process
US10279306B2 (en) 2014-07-10 2019-05-07 Climeworks Ag Steam assisted vacuum desorption process for carbon dioxide capture
US20170246588A1 (en) 2014-10-01 2017-08-31 Antecy B.V. Adsorption system with circulating adsorbent arrangement
EP3319998B1 (fr) 2015-07-10 2023-08-16 Climeworks AG Cellulose fibrillée à fonction amine pour adsorption de co2 et leurs procédés de fabrication
US20190060820A1 (en) 2016-03-01 2019-02-28 Antecy B.V. Shaped attrition resistant particles for co2 capturing and conversion
US10421039B2 (en) 2016-06-14 2019-09-24 Carbon Engineering Ltd. Capturing carbon dioxide
CN108201785A (zh) * 2018-02-02 2018-06-26 浙江大学 一种基于两相吸收剂的烟气二氧化碳吸收装置

Non-Patent Citations (1)

* Cited by examiner, † Cited by third party
Title
See references of EP2321034A4 *

Cited By (32)

* Cited by examiner, † Cited by third party
Publication number Priority date Publication date Assignee Title
US11504667B2 (en) 2008-08-21 2022-11-22 Carbon Engineering Ltd. Carbon dioxide capture method and facility
WO2014164738A3 (fr) * 2013-03-13 2014-12-24 Carbon Engineering Limited Partnership Recueil d'une solution caustique au moyen d'agrégats de cristaux de carbonate de calcium
US9975100B2 (en) 2013-03-13 2018-05-22 Carbon Engineering Ltd. Recovering a caustic solution via calcium carbonate crystal aggregates
US11007470B2 (en) 2013-04-18 2021-05-18 Climeworks Ag Low-pressure drop structure of particle adsorbent bed for improved adsorption gas separation process
US10427086B2 (en) 2013-04-18 2019-10-01 Climeworks Ag Low-pressure drop structure of particle adsorbent bed for adsorption gas separation process
US9751039B2 (en) 2013-04-18 2017-09-05 Climeworks Ag Low-pressure drop structure of particle adsorbent bed for adsorption gas separation process
WO2014170184A1 (fr) 2013-04-18 2014-10-23 Climeworks Ag Structure a faible chute de pression de lit adsorbant de particules pour un procede de separation de gaz par adsorption
US9637393B2 (en) 2014-05-19 2017-05-02 Carbon Engineering Limited Partnership Recovering a caustic solution via calcium carbonate crystal aggregates
US11014823B2 (en) 2014-05-19 2021-05-25 Carbon Engineering Ltd. Recovering a caustic solution via calcium carbonate crystal aggregates
US11667538B2 (en) 2014-05-19 2023-06-06 Carbon Engineering Ltd. Recovering a caustic solution via calcium carbonate crystal aggregates
US12054399B2 (en) 2014-05-19 2024-08-06 Carbon Engineering Ulc Recovering a caustic solution via calcium carbonate crystal aggregates
US10519041B2 (en) 2014-05-19 2019-12-31 Carbon Engineering Ltd. Recovering a caustic solution via calcium carbonate crystal aggregates
US10232305B2 (en) 2014-06-03 2019-03-19 Climeworks Ag Direct air capture device
US10279306B2 (en) 2014-07-10 2019-05-07 Climeworks Ag Steam assisted vacuum desorption process for carbon dioxide capture
WO2016005226A1 (fr) 2014-07-10 2016-01-14 Climeworks Ag Procédé de désorption sous vide assistée par de la vapeur pour capturer du dioxyde de carbone
US10421039B2 (en) 2016-06-14 2019-09-24 Carbon Engineering Ltd. Capturing carbon dioxide
US11014043B2 (en) 2016-06-14 2021-05-25 Carbon Engineering Ltd. Capturing carbon dioxide
WO2018083109A1 (fr) 2016-11-04 2018-05-11 Climeworks Ag Structure à faible chute de pression d'un lit d'adsorption de particules pour un procédé amélioré de séparation de gaz par adsorption
US11285425B2 (en) 2017-05-15 2022-03-29 Climeworks Ag Low-pressure drop structure of particle adsorbent bed for adsorption gas separation process
WO2018210617A1 (fr) 2017-05-15 2018-11-22 Climeworks Ag Structure à faible chute de pression de lit adsorbant de particules pour procédé de séparation de gaz par adsorption
US12006580B2 (en) 2018-04-25 2024-06-11 The University Of British Columbia Systems and methods for electrochemical generation of syngas and other useful chemicals
US11420149B2 (en) 2018-06-14 2022-08-23 Climeworks Ag Efficient method and device for adsorption/desorption of carbon dioxide from gas streams
WO2019238488A1 (fr) 2018-06-14 2019-12-19 Climeworks Ag Procédé et dispositif d'adsorption/désorption de dioxyde de carbone à partir de flux gazeux avec unité de récupération de chaleur
WO2020136211A1 (fr) 2018-12-28 2020-07-02 Vito Nv Capture et utilisation de dioxyde de carbone à médiation alcaline
EP3673972A1 (fr) 2018-12-28 2020-07-01 Vito NV Capture et utilisation de dioxyde de carbone à médiation alcaline
WO2020154518A1 (fr) 2019-01-23 2020-07-30 Blue Planet, Ltd. Compositions d'agrégats de carbonate et leurs procédés de préparation et d'utilisation
WO2020254208A1 (fr) 2019-06-21 2020-12-24 Climeworks Ag Structure d'adsorbant pour processus de séparation de gaz
WO2021099695A1 (fr) 2019-11-19 2021-05-27 Arkolia Energies Installation de production de méthane
WO2021239747A1 (fr) 2020-05-29 2021-12-02 Climeworks Ag Procédé de capture de dioxyde de carbone à partir d'air ambiant et structures adsorbantes correspondantes avec une pluralité de surfaces parallèles
WO2024006506A1 (fr) 2022-07-01 2024-01-04 W. L. Gore & Associates, Inc. Structure avec support externe pour lit adsorbant de particules pour processus de séparation de gaz d'adsorption
WO2024039641A1 (fr) 2022-08-15 2024-02-22 W. L. Gore & Associates, Inc. Structures et procédés pour améliorer la capture de dioxyde de carbone de l'air ambiant
WO2024129714A2 (fr) 2022-12-13 2024-06-20 W. L. Gore & Associates, Inc. Structure à faible chute de pression d'un lit d'adsorption de particules pour un procédé amélioré de séparation de gaz par adsorption

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WO2010022339A3 (fr) 2010-05-27
US9095813B2 (en) 2015-08-04
BRPI0917278B1 (pt) 2020-09-15
EP2321034B1 (fr) 2018-01-03
BRPI0917278A2 (pt) 2015-11-10
CN102202766A (zh) 2011-09-28
CN106621705A (zh) 2017-05-10
MX2011001898A (es) 2011-05-02
US20230158446A1 (en) 2023-05-25
CA2734786A1 (fr) 2010-02-25
EP2321034A2 (fr) 2011-05-18
US20190336909A1 (en) 2019-11-07
US20150336044A1 (en) 2015-11-26
US11504667B2 (en) 2022-11-22
EP2321034A4 (fr) 2012-11-28
CA2734786C (fr) 2017-11-07

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